US5567090A - Method and apparatus for separating solids from gas in a high pressure solids-gas stream utilizing a packed bed of the solids - Google Patents

Method and apparatus for separating solids from gas in a high pressure solids-gas stream utilizing a packed bed of the solids Download PDF

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Publication number
US5567090A
US5567090A US08/051,969 US5196993A US5567090A US 5567090 A US5567090 A US 5567090A US 5196993 A US5196993 A US 5196993A US 5567090 A US5567090 A US 5567090A
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United States
Prior art keywords
solids
gas
packed bed
vessel
gas stream
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Expired - Fee Related
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US08/051,969
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English (en)
Inventor
Arun K. Basak
Karukkampalayam M. Sellakumar
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Amec Foster Wheeler Energia Oy
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Foster Wheeler Energia Oy
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Priority to US08/051,969 priority Critical patent/US5567090A/en
Assigned to A. AHLSTROM CORPORATION reassignment A. AHLSTROM CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: SELLAKUMAR, KARUKKAMPALAYAM M., BASAK, ARUN K.
Priority to CA002121563A priority patent/CA2121563C/en
Priority to ES94106333T priority patent/ES2119929T3/es
Priority to AT94106333T priority patent/ATE167812T1/de
Priority to EP97116537A priority patent/EP0812613A3/de
Priority to JP6084880A priority patent/JPH06343810A/ja
Priority to EP94106333A priority patent/EP0621068B1/de
Assigned to FOSTER WHEELER ENERGIA OY reassignment FOSTER WHEELER ENERGIA OY ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: A. AHLSTROM CORPORATION
Priority to US08/691,912 priority patent/US5630680A/en
Publication of US5567090A publication Critical patent/US5567090A/en
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/24—Devices for removal of material from the bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B01D46/30—Particle separators, e.g. dust precipitators, using loose filtering material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/006—Separating solid material from the gas/liquid stream by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/16—Fluidised bed combustion apparatus specially adapted for operation at superatmospheric pressures, e.g. by the arrangement of the combustion chamber and its auxiliary systems inside a pressure vessel

Definitions

  • This invention relates to a method and an apparatus for handling high pressure material, particularly to a method for reducing pressure of a high-pressure solids-gas mixture and for separating the solids from the solids-gas mixture in a vessel.
  • the vessel is in communication with a reactor that is operated under a pressure of at least about 2 bars, and serves to maintain desired reactions, such as the combustion or gasification of fuel.
  • the vessel serves to remove ash or other particulate material from the reactor.
  • solids refers to all residues known to a person skilled in the art that may be obtained from reactions taking place in pressurized reactors, such as circulating fluidized bed reactors.
  • the main set of components of the RPDS are depressurizing piping ("transporting pipe”), a de-entrainment vessel wherein a packed bed of solid material is maintained for acting as a solids flow restriction at the end of the transporting pipe, and means for controlling the flow of the solids from the de-entrainment vessel.
  • An RPDS may be successfully utilized, for example, in connection with Pressurized Fluidized Bed reactors such as Pressurized Fluidized Bed Combustors or Gasifiers and processes executed therein.
  • Pressurized Fluidized Bed reactors such as Pressurized Fluidized Bed Combustors or Gasifiers and processes executed therein.
  • a Pressurized Fluidized Bed Gasifier which provides a partial gasification of fuel
  • a Fluidized Bed Combustor for oxidizing the residue char from the gasification
  • a transportation system for conveying the solids resulting from a partial gasification, such as char, to the final combustion
  • Any corresponding processes can be equipped with an RPDS as well.
  • the reactions take place at elevated pressure, e.g., 2-20 bar, and at elevated temperature, preferably about 1200° C., and residues are produced which should be subjected to further processing at lower pressure.
  • the solids discharged from a Pressurized Fluidized Bed reactor may be introduced to the RPDS either with or without first cooling the solids. If cooling is utilized, the temperature of the solids may be lowered even to about 300° C. temperature if the temperature of the solids-gas stream prior to introduction into the de-entrainment vessel is about 300°-1200° C. (e.g., about 300°-799° C.); otherwise, the temperature is still reduced to below that of the reactor, e.g., to about 800°-1200° C.
  • a necessary feature of the RPDS system in order to achieve continuous movement of the solids with a simultaneous pressure drop of the gas, is to cause the gas to flow faster than the solids in the piping.
  • the RPDS usually smoothly and reliably de-pressurizes the solids. It also has some advantages over a lockhopper as a depressurization device (e.g., the flow of the solids is continuous, and valve maintenance time and costs are decreased).
  • the gas flow rate is increased to too great an extent, the whole de-pressurizing process is handicapped due to the fluidization of the solids in the de-entrainment vessel.
  • the fluidization of the solids is detrimental to the function of the device since restriction to solids flow is destroyed, and the flow of the solids becomes uncontrollable. Therefore, it is very important to guard against fluidization of solids, to guarantee the smooth running of the entire process.
  • the invention provides a method and an apparatus to ensure the proper function of a de-pressurization system utilizing an RPDS in various process situations.
  • the present invention -in a significant departure from the conventional system discussed above--has solved the problem of deterioration of de-pressurization capability even when the conditions under which fluidization would normally take place if the conventional technique existed, by preventing the possibility of fluidization of the solids. This is accomplished in accordance with the method of the present invention by decreasing the flow velocity of the gas prior to or when discharging the gas into the packed bed of solids in the de-entrainment vessel.
  • the cross-sectional area of the opening through which the gas and solid streams are discharged into the bed of solids in the de-entrainment vessel is larger than the cross-sectional area of the pipe introducing the gas and solid streams into the de-entrainment vessel and used for pressure release of the gas.
  • the reduction of the velocity of the gas discharging into the de-entrainment vessel is preferably accomplished immediately prior to or when discharge of the gas takes place since it is advantageous to maintain a higher velocity as long as possible in order to achieve a large enough pressure loss in the transporting pipe.
  • the discharge of the gas-solids stream into the de-entrainment vessel can be designed to be optimal independently of the pressure reduction effects in the transporting pipe.
  • a method of reducing the pressure of a high pressure solids-gas stream, and separating the solids from the solids-gas stream utilizes a de-entrainment vessel including a packed bed of solids, a solids outlet, a gas outlet above the level of the packed bed connected to a low pressure area, and an inlet for the solids-gas stream into the vessel.
  • the method comprises the steps of substantially continuously: (a) introducing the high pressure solids-gas stream into the de-entrainment vessel through the inlet so that the gas of the solids-gas stream flows faster than the solids, to provide a pressure drop of the gas; (b) causing the gas from the solids-gas stream of step (a) to flow through the packed bed of solids; (c) causing the velocity of the gas to decrease during, or just prior to, introduction of the gas into the packed bed of solids, to minimize the possibility of fluidization of the solids; (d) discharging the gas separated from the solids-gas stream, after it has passed through the packed bed, through the gas outlet and transporting it to a low pressure area; and (e) discharging solids from the vessel below the level of the packed bed.
  • the temperature of the gas-solids stream, and bed solids is between about 800°-1200° C.
  • the gas-solids stream typically has a pressure of about 2-20 bar, and steps (d) and (e) are typically practiced to discharge the separated gas and solids to substantially atmospheric pressure areas.
  • the method may also include the further step of dividing the solids-gas stream into a plurality of streams prior to step (b). There also may be the additional step of further minimizing the possibility of fluidization of the solids by passing the gas, after or simultaneously with step (b), through an element permeable to gas but substantially impermeable to solids within the gas-solids stream or the packed bed.
  • apparatus for reducing the pressure of a high pressure solids-gas stream and separating the solids from the solids-gas stream.
  • the apparatus comprises the following elements: A substantially vertical de-entrainment vessel having a bed of packed solids therein, disposed at a level within the vessel, and a side wall.
  • a transporting pipe having a first cross-sectional area and containing the solids-gas stream therein at a super-atmospheric pressure.
  • Inlet means connected to said transporting pipe, and disposed within the de-entrainment vessel, and including a discharge opening below the level of the bed of packed solids, the inlet means at the discharge opening having a second effective cross-sectional area significantly greater than the first cross-sectional area, so as to minimize the possibility of fluidization of the solids.
  • a gas outlet from the vessel is located above the level of the bed of solids, and is connected to an area having a lower pressure than the pressure in the transporting pipe; and a solids outlet from the vessel is located below the level of the bed of solids, and is connected to an area having a lower pressure than the pressure in the transporting pipe.
  • the inlet means may include a gradually expanding cross-sectional area section (e. g., right circular cone) at the discharge opening.
  • a plurality of openings may be provided in the cone, below the level of the packed bed of solids, through which gas flows toward (that is with at least a velocity component toward) the vessel wall.
  • the apparatus also preferably further comprises additional means, for substantially preventing fluidization, comprising a substantially gas permeable and substantially solids impermeable element operatively connected to the inlet means adjacent the discharge opening disposed in the pathway of gas from the inlet means to the gas outlet.
  • the fluidization preventing means element may be directly connected to the inlet means adjacent the discharge opening, and extends from the inlet means toward the vessel wall; in fact, the fluidization preventing means element may cover substantially the entire area between the inlet means and the vessel side wall, substantially defining the upper level of the packed bed of solids.
  • the fluidization preventing means element typically is selected from perforated plates, wire mesh screens, and filtering means (e.g., ceramic filters).
  • the fluidization preventing means element may also have uniform or varying gas permeability. For example, the gas permeability of the fluidization preventing means element may be lowest closest to the inlet means, and greatest closest to the vessel side wall, and may gradually increase from the inlet means toward the vessel side wall.
  • the transporting pipe may optionally comprise a single transporting pipe having the first cross-sectional area
  • the inlet means may comprise a plurality of inlet elements connected to and branching from the single transporting pipe.
  • the inlet elements collectively having a second cross-sectional area significantly greater than the first cross-sectional area.
  • the solids outlet may comprise a plurality of outlet elements
  • the gas outlet may comprise a plurality of outlet elements.
  • the apparatus described above may be in combination with a pressurized fluidized bed reactor having a pressure of about 2-20 bar, and connected to the transporting pipe. Also, there optionally is a cooling means disposed between the reactor and the inlet means for cooling the temperature of the solids-gas stream to about 300°-799° C.
  • an apparatus for the same purpose comprising the following elements: A substantially vertical de-entrainment vessel having a bed of packed solids therein, disposed at a level within the vessel, and a side wall.
  • a transporting pipe containing the solids-gas stream therein at a super-atmospheric pressure.
  • Inlet means connected to the transporting pipe, and disposed within the de-entrainment vessel, and including a discharge opening below the level of the bed of packed solids.
  • a solids outlet from the vessel is located below the level of the bed of solids, and is connected to an area having a lower pressure than the pressure in the transporting pipe; and means, for substantially preventing fluidization, comprising a substantially solids impermeable and a substantially gas permeable element is operatively connected to the inlet means and extends toward the vessel side wall.
  • the fluidization means is preferably as described above, with respect to the previous apparatus aspect of the invention.
  • FIG. 1 is a schematic side cross-sectional view of a first exemplary embodiment of apparatus according to the present invention, for practicing a method of gas-solids stream pressure reduction, and solids and gas separation, according to a method of the invention;
  • FIG. 2 is a view like that of FIG. 1 for a second exemplary embodiment
  • FIG. 3 is a view like that of FIG. 1 for a third exemplary embodiment, with the bottom of the vessel cut away for clarity of illustration;
  • FIG. 4 is a view like that of FIG. 1 for a fourth exemplary embodiment of apparatus according to the invention.
  • the invention exemplary apparatus illustrated in FIG. 1 for conveying solid material particles in gas from higher pressure to lower, e.g., atmospheric, pressure, utilizing an RPDS comprises as a main component a vertical de-entrainment vessel 1, and means for conveying the solids-and-gas stream through transporting pipe 2 into the de-entrainment vessel 1.
  • the transporting pipe 2 is operatively connected to a pressurized reactor, such as the pressurized fluidized bed reactor 10 shown schematically in FIG. 1, from which the stream of solids and gas is discharged.
  • reactor 10 reactions take place at high pressure, e.g., about 2-20 bar, and at high temperature, e.g., about 1200° C.
  • the gas is arranged to flow faster than the solid material in the transporting pipe 2 before and/or while discharging into the de-entrainment vessel 1.
  • the transporting pipe 2 is, according to the embodiment illustrated in FIG. 1, located in the upper section of the de-entrainment vessel 1, and is substantially vertical; however, pipe 2 may also be positioned in other locations and with other orientations with respect to vessel 1.
  • An inlet means 5 with expanding section 6 is attached at the end of the transporting pipe 2.
  • the expanding section (e.g., right circular cone) 6 may also include a plurality of discharge openings 7 of suitable size and shape, adjacent the free open end (and end discharge opening) thereof, as seen in FIG. 1. Both the end of cone 6 and the openings 7 are below the level of particles in bed 8.
  • the flow area determined by the periphery walls of the section 6 increases as the solids and gas in the transporting pipe 2 flow through the inlet means 5.
  • the gas forces its way towards the circumferential edge or edges at the end of the inlet means 5 and separates from the solids.
  • the expanding area provides an increased area for the gas to separate from the solids, which lowers the velocity of the gas.
  • the elements 2 and 6 are preferably substantially circular in cross section (e.g., the element 6 being conical), but may have a polygon or other cross-sectional shape.
  • the gas separated from the solids in vessel 1 is subsequently vented out of the vessel 1 through an outlet 4.
  • the gas outlet 4 is situated in a gas space 9 of the de-entrainment vessel 1 above the level of the bed of solids 8, and may be equipped with an appropriate conventional filter element 11, if desired.
  • the gas flowing through outlet 4 is discharged to a lower pressure (e.g., atmospheric) area.
  • the solids separated from the gas are continuously removed from the de-entrainment vessel 1 through a solids outlet 3, preferably situated in the lower section of the vertical de-entrainment vessel 1.
  • the outlet 3 is, according to the embodiment illustrated in FIG. 1, located along the vertical center line of the de-entrainment vessel 1, but within the scope of the present invention it may be located in any suitable location, and several outlets may be employed instead of the one (3) illustrated in FIG. 1.
  • the outlet 3 may have a conventional control device 12, and is connected to a lower (e.g., atmospheric) pressure area.
  • FIG. 2 there is illustrated another exemplary embodiment of apparatus according to the present invention.
  • the hot solids and gaseous materials from reactor 18 may pass through a cooling means 19, and then are transported into a substantially vertical de-entrainment vessel 21 through a transporting pipe 22 connected to an inlet means 25 of the de-entrainment vessel 21.
  • the inlet means 25 is attached at the end of the transporting pipe 22.
  • the flow area increases as the solids and gas in the transporting pipe 22 flow through the inlet means 25. The gas forces its way towards the circumferential edge or edges at the end of the inlet means 25 and separates from the solids.
  • the risk of any local fluidization in vessel 21 is essentially eliminated by the preventing means 26 attached to the inlet means 25 at its lower end.
  • the preventing means 26 may also be attached to the periphery, or edge, of the inlet means 25.
  • the preventing means 26 acts as a restraint on top of the packed bed of solids 28 thus minimizing the risk of local fluidization as the gas pushes its way up through a section of the topmost layer of solids bed 28 around the periphery of the inlet means 25.
  • the preventing means 26 is a gas permeable plate or disc, e.g., made from a wire mesh screen or perforated metal or ceramic plate, or it may comprise a filter, such as a ceramic filter which separates any particles which tend to be entrained by the gas from bed 28.
  • the gas separated from the solids in de-entrainment vessel 21 is subsequently vented out of the vessel 21 through an outlet 24 for gas.
  • a low gas velocity in inlet means 25 is necessary to avoid local fluidization or formation of channels in the packed bed of solids 28.
  • the solids separated from the gas are continuously removed from the de-entrainment vessel 21 through a solids outlet 23 situated--in the particular embodiment of FIG. 2--adjacent to a side wall 30 of the de-entrainment vessel 21.
  • FIG. 3 shows still another exemplary embodiment of apparatus according to the invention.
  • a substantially upright (vertical), substantially circular in cross-section de-entrainment vessel 31 is equipped with a gas and solids transporting pipe 32 which is substantially horizontal where it enters the de-entrainment vessel 31 through a side wall 40, and includes an inlet means 35, provided with a fluidization preventing means 36, at the bottom of a vertical section of pipe 32.
  • a gas outlet 34 is also provided.
  • the outlet for separated solids is not shown in FIG. 3; however, any suitable arrangement known by a person skilled in the art may be applied.
  • the inlet fluidization preventing means 36 is permeable to gas and substantially impermeable to solids.
  • the fluidization preventing means 36 preferably has almost no gas permeability (e.g., is essentially solid) at the region thereof nearest the inlet means 35, with gradually increasingly greater gas permeability from the inlet 35 to the side wall 40 of the vessel 31. In this way it is possible to gain the benefits of the present invention substantially without having any enlargement of the discharge opening 35 itself, but merely by having the fluidization preventing means 36 first act as an enlarged flow path of the gas thus causing the reduced velocity and, after the gas permeability of the preventing means 36 is increased, then acting as a gas permeable, solid impermeable, device.
  • Gas outlet 34 may be provided with a filtering device (i.e., like device 11 in FIG. 1), and is well above the level of particle bed 38.
  • FIG. 4 illustrates still another exemplary embodiment of apparatus according to the present invention which is preferred for the transport of finer solids materials.
  • multiple (branch) transporting lines 423, 422, 421 from transporting pipe 42 are adapted to discharge the solids and gaseous material into the interior of the de-entrainment vessel 41, each line 421, 422, 423 provided with its own inlet means (e.g., cones) 453, 452, and 451, respectively.
  • a fluidization preventing means 46 e.g., a perforated plate or wire mesh screen, or ceramic filter
  • the separated-out gas is subsequently vented out of the de-entrainment vessel 41 through gas outlets 441, 442.
  • the number of the inlets 421-423 and outlets 441-442 is dependent upon the process parameters.
  • the desired lower gas velocity is accomplished by splitting the initial stream in pipe 42 into a plurality of lines (e.g., 2, 3, or more), while simultaneously maintaining the desired pressure reduction.
  • a plurality of solids outlets 43 are also provided, the number depending upon the process parameters and the shape of the vessel 41.
  • a splitting means 40 is provided in the transporting pipe 42 above vessel 41.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Filtering Of Dispersed Particles In Gases (AREA)
  • Separating Particles In Gases By Inertia (AREA)
US08/051,969 1993-04-22 1993-04-22 Method and apparatus for separating solids from gas in a high pressure solids-gas stream utilizing a packed bed of the solids Expired - Fee Related US5567090A (en)

Priority Applications (8)

Application Number Priority Date Filing Date Title
US08/051,969 US5567090A (en) 1993-04-22 1993-04-22 Method and apparatus for separating solids from gas in a high pressure solids-gas stream utilizing a packed bed of the solids
CA002121563A CA2121563C (en) 1993-04-22 1994-04-18 Method and apparatus for separating solids from gas in high pressure solids-gas stream utilizing a packed bed of the solids
EP97116537A EP0812613A3 (de) 1993-04-22 1994-04-22 Verfahren und Vorrichtung zur Behandlung von Material unter Hochdruck
AT94106333T ATE167812T1 (de) 1993-04-22 1994-04-22 Verfahren und vorrichtung zur entspannung eines unter hohem druck stehenden, feststoffpartikel enthaltenden gasstroms
ES94106333T ES2119929T3 (es) 1993-04-22 1994-04-22 Procedimiento y aparato para la reduccion de la presion de una corriente de gas-solidos a alta presion.
JP6084880A JPH06343810A (ja) 1993-04-22 1994-04-22 高圧の固体／気体の流れを減圧して固体を分離する方法と装置
EP94106333A EP0621068B1 (de) 1993-04-22 1994-04-22 Verfahren und Vorrichtung zur Entspannung eines unter hohem Druck stehenden, Feststoffpartikel enthaltenden Gasstroms
US08/691,912 US5630680A (en) 1993-04-22 1996-08-01 Method and apparatus for separating solids from gas in a high pressure solids-gas stream utilizing a packed bed of the solids

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US08/051,969 US5567090A (en) 1993-04-22 1993-04-22 Method and apparatus for separating solids from gas in a high pressure solids-gas stream utilizing a packed bed of the solids

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US08/691,912 Expired - Fee Related US5630680A (en) 1993-04-22 1996-08-01 Method and apparatus for separating solids from gas in a high pressure solids-gas stream utilizing a packed bed of the solids

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US (2) US5567090A (de)
EP (2) EP0621068B1 (de)
JP (1) JPH06343810A (de)
AT (1) ATE167812T1 (de)
CA (1) CA2121563C (de)
ES (1) ES2119929T3 (de)

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US6632063B1 (en) * 1999-03-01 2003-10-14 Norsk Hydro Asa Method and an arrangement for filing a silo
US20040011203A1 (en) * 2001-03-01 2004-01-22 Fitch Thomas M Filtration media of porous inorganic particles
US20040139858A1 (en) * 2001-03-01 2004-07-22 Phillips Plastics Corporation Filtration media of porous inorganic particles
US7041159B2 (en) 2003-08-04 2006-05-09 Phillips Plastics Corporation Separation apparatus
US7166140B2 (en) 2003-10-22 2007-01-23 Phillips Plastics Corporation High capture efficiency baffle
TWI499448B (zh) * 2009-04-20 2015-09-11 Southern Co 連續細塵減壓系統
US9950939B2 (en) * 2012-01-27 2018-04-24 Ohio University Technique for removal of organics and dissolved solids from aqueous medias via supercritical treatment

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ATE425738T1 (de) * 1999-11-17 2009-04-15 Boston Scient Ltd Miniaturisierte vorrichtungen zur abgabe von molekulen in einer tragerflussigkeit
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EP0621068B1 (de) 1998-07-01
US5630680A (en) 1997-05-20
CA2121563C (en) 1999-03-30
CA2121563A1 (en) 1994-10-23
EP0812613A2 (de) 1997-12-17
JPH06343810A (ja) 1994-12-20
ATE167812T1 (de) 1998-07-15
EP0621068A1 (de) 1994-10-26
EP0812613A3 (de) 1998-02-25

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